1. Introduction - Firenze University Press

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Fig. 1. Solution diagram of „four end”, average integration [9] The paper includes the analysis and comparison with a classic gas turbine of an air separation unit (ASU). The computations results obtained with ASU model were compared with the results obtained using an autonomous gas turbine model. The air separation model will be used to build the models of oxy-combustion power plants. 2. Model of the air separation unit (ASU) and assumptions for calculations Air separation unit structure consists of: counter-flow air heater (APH), air compressor (C), expander (EX), electric generator (G) and "four-end" type membrane (M). The expander drives the air compressor. Depending on the assumed quantities the expander and compressor can give or take electricity from the grid. The structure of the air separation unit is shown in Figure 2. The characteristic basic quantities of the air separation unit and autonomous gas turbine are gathered in Table 1. Fig. 2. Scheme of the air separation unit (ASU) 37
Table 1. Characteristic quantities for investigated air separation unit (ASU) Name Symbol Value Unit Ambient pressure Ambient temperature Membrane working temperature pot tot tmem 101.3 kPa o 20 C o 750;850 C Stream of separated oxygen m O2 107.56 kg/s Oxygen recovery rate R 40÷100 % Compressor pressure ratio k 2÷30 - Compressor isentropic efficiency iS 0.88 - Expander isentropic efficiency iT 0.9 - Generator efficiency g 0.99 - It was assumed for the calculations that the air taken from environment is a dry gas consisting of 21% oxygen and 79% nitrogen (volumetric composition). The characteristic quantities gathered in Table 1 were used for computations performed on a "fourend" membrane air separation unit model, made in GateCycle TM software. The built-in components were used to build the air separation unit model. The quantity that determinates the value of the mass flow rate in the entire ASU model is a mass flow rate of oxygen. This mass flow rate is approximately the same as the oxygen mass flow rate feeding an oxy boiler working in a 460 MW power plant. It was assumed that through the membrane flows pure oxygen. The structure of an autonomous gas turbine as opposed to a structure of ASU shown in Figure 2 does not contain a "four-end" type membrane. In the autonomous gas turbine model the assumption concerning a compressor, expander and air heater are the same as in the ASU model. The air mass flow rate in both models are the same, the difference is only in the mass flow rate and composition of gas flowing into the expander. In the ASU model the composition and mass flow rate of the gas is different from air because some oxygen is separated from air in the membrane. In the autonomous gas turbine model the mass flow rate and composition of gas flowing into the expander is the same as mass flow rate and composition of air leaving the air heater. 3. The results of calculations of air separation unit and autonomous gas turbine The air mass flow rate depends on the separated in membrane oxygen mass flow rate ( m O2 ), oxygen recovery rate (R) and mass content of oxygen in the air ( g O2air ). The relationship between these quantities is as follows: m O2 1a , (2) R gO2air m Next the air is compressed by the compressor. Effective power required to drive the compressor depends on the air mass flow rate ( 1a m ), the air temperature ( 1a T ), the average specific heat ( ~c p ), K 1 the compressor pressure ratio ( K ), the heat capacity ratio contained in the factor ( K ), K the compressor isentropic efficiency ( iK ) and the compressor mechanical efficiency ( mK ). The equation showing the relationship between these quantities is as follows: 38
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Proceedings e report 90
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ECOS 2012 : the 25 th International
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Advisory Committee (Track Organizer
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The 25 th ECOS Conference 1987-2012
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VOLUME VI CONTENT VI. 1 CARBON CAPT
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Page 16 and 17: » Personal transportation energy c
Page 18 and 19: » Excess enthalpies of second gene
Page 20 and 21: VOLUME IV IV . 1 - FLUID DYNAMICS A
Page 22 and 23: » Exergy analysis and genetic algo
Page 24 and 25: » Optimal lighting control strateg
Page 26 and 27: » Stability and limit cycles in an
Page 28 and 29: PROCEEDINGS OF ECOS 2012 - THE 25 T
Page 30 and 31: Fig. 2. The exergy destruction of M
Page 32 and 33: ineffectiveness of the catalyst, in
Page 34 and 35: [ P EXmth EX SNG] ESR F where EXm
Page 36 and 37: Fuel inputkW 728221 203771 237719 3
Page 38 and 39: Not only at desined Rc (the ratio o
Page 40 and 41: 4. DISCUSSION The graphic exergy an
Page 42 and 43: Figure 9(a) illustrates the energy
Page 44 and 45: Engineering Technical Conferences &
Page 46 and 47: generally there are four kinds of m
Page 48 and 49: However, even under the off-design
Page 50 and 51: Fig. 3. 600MW supercritical coal-fi
Page 52 and 53: CO2 rich loading(molCO2/molMEA) 0.4
Page 54 and 55: Net efficiency (%) 40.28 30.29 26.4
Page 56 and 57: Fig. 11. Schematic diagram of heat
Page 58 and 59: 28.67%. In addition, through heat i
Page 60 and 61: Applied Thermal Engineering 2010;30
Page 62 and 63: Abstract: PROCEEDINGS OF ECOS 2012
Page 66 and 67: K ~ K 1 eK 1a p K 1a iK mK
Page 68 and 69: Oxygen recovery rate, % 105 95 85 7
Page 70 and 71: Calculated optimal compressor press
Page 74 and 75: The net amount of the flue gas leav
Page 76 and 77: Figure 3. Idea for lignite drying b
Page 78 and 79: Energy efficiency, % 34,00 33,00 32
Page 80 and 81: points efficiency increase related
Page 82 and 83: Figure A1b. Thermoflex flow sheet o
Page 84 and 85: Figure A3a. Thermoflex flow sheet o
Page 86 and 87: Figure A4. Thermoflex flow sheet of
Page 90 and 91: 2.1. Life Cycle Assessment 2.1.1. G
Page 92 and 93: these factors. A sensitivity analys
Page 94 and 95: methane slip contributes to 13% of
Page 96 and 97: As can be seen in Fig. 5 the impact
Page 98 and 99: References [1] Eurobserv’er, The
Page 102 and 103: in which CO2 is separated from H2,
Page 104 and 105: dimensions of water droplets and wa
Page 106 and 107: Temperature (°C) 8 7 6 5 4 3 2 1 0
Page 108 and 109: 4. Conclusions In the present paper
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0.5 - 0.7 kg/kg, resulting typicall
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3.3 - Utilising waste heat All exis
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4.5 - Suomusjärvi olivine deposits
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material will change from a few % t
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Fig. 5 Schematic diagram of the PFB
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8. Combined SO2 capture and CO2 min
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Fig. 10 Carbonate- (left) and sulph
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[13] Ekdahl, E., Idman, H. Statemen
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Abstract: PROCEEDINGS OF ECOS 2012
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HEAT Fig. 1. Scheme and main reacti
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(raw) materials pre-heating and AS
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Fig 3- Aspen Plus® model 110
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Table 4. Elemental and XRD analysis
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the ÅA CSM route. The content of M
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moisture - 0,2237 ash - 0,0876 LHV
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2.2 CFB plant For the current momen
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The CO2 emission factor which indic
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The CO2 emission factor calculated
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Appendix A Fig A.1. Simulation mode
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(b) Fig. A.2. Simulation model of C
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Table A.1. Calculated parameters at
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References [1] Pfaff I., Oexmann J.
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with a CC installation could be avo
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2.3. Basic CHP plant indices. The b
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3. Off-design calculations The main
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Fig. 6. CHP plant efficiency Fig. 7
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amount of steam delivered to the he
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[5] Lukowicz H., Mroncz M.: Analysi
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water removal is feasible by coolin
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Figure 2. Sketch of the suggested P
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a b Figure 5. a) Exergy balance of
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The basis of comparison of each met
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Figure 7a. Impact of S/CATR on PCU
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However, more energy duty is requir
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3.1. JACOBIAN-ASPEN Interface ASPEN
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Fig. 3. Triple Pressure Bottoming S
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As seen from Table 1, the mass flow
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4. Conclusion Fig. 5. Partial Emiss
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[19] Yantovski E., Shokotov M., Sho
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investigation and the developing of
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University of L’Aquila and German
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hydrogen combustion technology at d
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eversibility of a pre-treated synth
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Fig. 1. TG curves collected for spe
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(see Fig 5). Carbon dioxide uptake
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period is reduced to the first 15 c
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CO2 capture capacity up to 150 th c
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the way for biogas utilisation is t
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projectand is described in the foll
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4. Pilot plant tests In order to de
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Concerning the absorption reaction,
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with Regeneration (AwR), consists i
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[25] Aspen Plus 2004.1. Cambridge,
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systems for fuel drying waste strea
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heated in a heat exchanger placed i
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Fig. 2. Lower heating value of fuel
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Acknowledgements The results presen
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large amount of CO2 [1,5-7]. APCr a
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N 1 i ( x x i n 1 m ) 2.3. Carbon
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DTA analysis of the untreated APCrs
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Table 4. Relative Error (%) of the
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CaO HCl CaCl H O 193kJ / mol (
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[1] M. Fernández Bertos, S.J.R. Si
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2. Process development 2.1. Backgro
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to dissolve the chloride salts prec
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The remaining 25% (5 ml/min) of the
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Table 6. Experimental conversions o
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p p 1 1. 5 p H 1 1. 5 2O p mi
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Calculating from the Aspen Plus mod
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[11] Mattila, H.-P., Experimental s
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Mg2SiO4(s) + 2CO2(g) →2MgCO3(s) +
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(Mg/Fe) of the mineral rock, Mg-sil
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Figure 2. Effect of Mg/Fe ratio of
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Figure 4 shows that an increase in
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Figure 5. Process flow diagram of M
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2. Only cold utility is needed belo
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extraction process at 400 °C (~ 62
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Table A2. Extraction equations and
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[13] Teir S, Kuusik R, Fogelholm CJ
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In the area of coal technologies al
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Tabel 1. Characteristics quantities
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N m eT 4a ~ T cp T4a 1 ( K
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Auxiliary power rate of ASU, % 40 4
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[8] Buhre B.J.P., Elliott L.K., She
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1.1 - Cement Manufacturing The ceme
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2. Numerical model The purpose of t
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-0.309x15.77x2 2.085x3 240x4 12.53x
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Table 4 - Results of the optimizati
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PROCEEDINGS OF ECOS 2012 - THE 25 T
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1. Define the studied system (in th
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cycle) or a lignin extraction plant
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limiting factor for the maximum siz
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Table 5. Key data for the four ener
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Global CO 2 emissions [ktonnes/yr]
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for biofuels and the investment cos
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The possibility to capture CO2 from
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[17] Berglin N, Andersson L. Proces
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Therefore NL Agency (an agency of t
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2.2.2. Pinch analysis Pinch analysi
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3. Case study 3.1. Plant and proces
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Te 1000 mp era 900 tur 800 e [°C 7
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Application of the approach led to
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The advantage of dynamic models is
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e equal at both time intervals and
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2.5. Selecting the number of TSs Se
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A) Time Slices for solar thermal en
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The first step of procedure is to p
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cTSs demand TS solar TSs 0 2 4 6 8
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In the presented paper a framework
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[5] Erdil E, Ilkan M, Egelioglu F.
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PROCEEDINGS OF ECOS 2012 - THE 25 T
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district energy network simulation
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were decreased by 10°C.All scenari
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Site 3 Heat sources Heat load Site
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3.2.2. Input data and assumptions A
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Fig.7 shows the operation forecast
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[13] TERMIS Operation User Guide, 7
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Polygeneration is a term used to de
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The increase in energy utilization
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are available for an entire year, 8
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6. Extensions to core methodology 6
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thermal storage and possible suppor
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laterites. Ore Geology Reviews, v.
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gasification [15], hybrid biomass g
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the second reactor. In this unit, s
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The variables effect was evaluated
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atio, as well as the shift-syngas f
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Fig. 4. Effect of operating tempera
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SDG has slight effect on the syngas
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[26.] Castle WF. Air separation and
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1. Introduction - Firenze University Press

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